US6699708B1 - Process and device for treating a mixture of substances containing organic matter - Google Patents

Process and device for treating a mixture of substances containing organic matter Download PDF

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US6699708B1
US6699708B1 US09/830,425 US83042501A US6699708B1 US 6699708 B1 US6699708 B1 US 6699708B1 US 83042501 A US83042501 A US 83042501A US 6699708 B1 US6699708 B1 US 6699708B1
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mixture
reactor
substances
air
supplied
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Patrick Muller
Christian Widmer
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
    • C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
    • C05F17/90—Apparatus therefor
    • C05F17/95—Devices in which the material is conveyed essentially vertically between inlet and discharge means
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
    • C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
    • C05F17/90—Apparatus therefor
    • C05F17/964—Constructional parts, e.g. floors, covers or doors
    • C05F17/971—Constructional parts, e.g. floors, covers or doors for feeding or discharging materials to be treated; for feeding or discharging other material
    • C05F17/979—Constructional parts, e.g. floors, covers or doors for feeding or discharging materials to be treated; for feeding or discharging other material the other material being gaseous
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
    • C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
    • C05F17/90—Apparatus therefor
    • C05F17/964—Constructional parts, e.g. floors, covers or doors
    • C05F17/971—Constructional parts, e.g. floors, covers or doors for feeding or discharging materials to be treated; for feeding or discharging other material
    • C05F17/986—Constructional parts, e.g. floors, covers or doors for feeding or discharging materials to be treated; for feeding or discharging other material the other material being liquid
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/02—Form or structure of the vessel
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/02—Percolation
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/26—Conditioning fluids entering or exiting the reaction vessel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/40—Bio-organic fraction processing; Production of fertilisers from the organic fraction of waste or refuse

Definitions

  • the invention relates to a process for treating a mixture of substances containing structured constituents and organic matter in accordance with the preamble of claim 1 , and a device in particular for carrying out this process.
  • Such a process is, for example, utilized for treating residual waste matter.
  • a waste matter treatment method is described, wherein the residual waste matter is treated in a percolator.
  • organic constituents, inorganic substances and in a given case water-soluble fatty acids are leached from the waste matter by an extracting or washing agent.
  • the residue is withdrawn from the percolator and, following a subsequent drying, supplied to combustion or dumped.
  • an agitator or circulating apparatus is provided in the reactor, whereby the waste matter is mixed thoroughly in a vertical direction (in parallel with the direction of flow of leaching fluid and process air) and also displaced in the direction of transport.
  • the invention is based on the object of furnishing a process for treating a mixture of substances containing structured constituents and organic matter, and a device wherein sufficient decomposition of the organic proportion takes place at minimum expense in terms of device technology.
  • the reactor may have a substantially more simple construction than in the above described prior art because it is not necessary to provide an agitator for lateral mixing.
  • the forces are preferably introduced from the peripheral area of the reactor, for example through a suitably designed discharge means or by means of injected gas, preferably pressurized air. In particular when pressurized air is used, shear forces are also applied to the bulk material, whereby the surface of the heap material is reorganized and particles of the mixture of substances are separated into fibers.
  • the reactor nay be employed as a percolator and dryer without any restructuring or modifications becoming necessary.
  • the mixture of substances is preferably circulated at least in part, so that shear forces are introduced due to the conveyor elements bringing about the circulation.
  • the flow management according to the invention makes it possible to design the reactor with a high degree of compactness, wherein it is possible to position all of the feeding and discharging means at the head or bottom portion of the reactor.
  • the forces for prevention of channel formation and the shear forces required for surface reformation and for tearing open the particles are applied through a pressure gas, preferably pressurized air, which is injected into the bulk material (heap material) from the peripheral area of the reactor.
  • a pressure gas preferably pressurized air
  • the pressurized air and the process air are supplied through nozzles arranged in the foot portion and/or in the bottom portion of the reactor.
  • the mixture of substances passes through the reactor essentially vertically (in parallel with the direction of gravity) or horizontally, so that the mixture of substances is guided approximately in parallel or in a flow transversal to the process air.
  • the leaching fluid is preferably supplied through a distributor in the head portion of the reactor.
  • the pressurized air is supplied at a pressure of more than 2 bar, preferably more than 4 bar, whereas a pressure of 0.5 bar is customarily applied to the process air.
  • the nozzles for introduction of the process air and/or pressurized:air may advantageously be controlled individually, so that a specific pressurized air profile may be adjusted across the reactor cross-section.
  • pressurized air for introducing shear forces and for preventing channel formation has the advantage of the atmospheric oxygen required in the bulk material for the aerobic process being supplied concurrently, so that the pressurized air basically fulfills a twofold function:
  • the forces for preventing channel formation in the bulk material are, for example, supplied through a discharge means arranged at the bottom portion of the reactor.
  • This discharge means may, for example, be a scraper floor installation or a similar conveyor means for discharging the mixture of substances by layers.
  • This variant has the additional advantage of feeding and discharging openings in the bottom portion of the reactor being kept free owing to the advance movement of the discharge means, so that the leaching fluid may exit and pressurized air or process air, respectively, may penetrate into the bulk material.
  • a discharge means a worm conveyor carpet, a walking floor, silo filler means etc. may also be used. These discharge means may, of course, also be used in the above described embodiment with pressurized air.
  • the dwell time of the mixture of substances inside the reactor may be determined with high precision in the case of continuous process management, so that the passage times with respect to the biological decomposition may be optimized.
  • only a mean dwell time value could be determined due to the longitudinal and transversal mixing by means of the agitator.
  • the laden process air or the laden pressurized air, respectively, are supplied to a waste gas purification wherein organic constituents are separated and the purified air is recycled into the process.
  • the energy balance of the installation may be further improved if the laden leaching agent is supplied to a sewage water purification.
  • the latter may contain a biogas installation wherein conversion of the organic matter into biogas takes place. Through energetic coupling of the liberated biogas, the process according to the invention may be designed to be largely self-sufficient as regards energy.
  • the mixture of substances containing organic matter is subjected to a so-called hydrolysis wherein, through co-operation of air and leaching fluid, the organic material is dissolved and acidified as a result of aerobic, thermophilic heating by the air and carried off by the leaching fluid. I.e., decomposition of the organic constituents takes place as a result of setting a certain humidity and supplying clean air.
  • Further processing of the mixture of substances provides for drying of the residue in accordance with the invention.
  • drying may be effected at minimum energetic expense by aerobic, thermophilic heating of the residue in the reactor.
  • the mixture of substances may either be subjected to application of clean air in the reactor, so that by the resulting aerobic heating water vapor is discharged via the supplied air; and the residue is dried.
  • Drying and hydrolysis in one single reactor is, however, under the condition of batch-type operation which should be viable only in smaller installations.
  • a separate reactor (dryer) is provided for aerobic, thermophilic heating of the residue from hydrolysis.
  • these two reactors may also be arranged behind each other in n-fold succession in a single container, so that several hydrolysis/drying steps may follow in succession.
  • the energy balance of the installation may be further improved if the laden leaching agent of a purification of sewage water is supplied.
  • the latter may contain a biogas installation in which conversion of the organic matter into biogas takes place. Through energetic coupling of the liberated biogas, the process according to the invention may be designed to be self-sufficient as regards energy.
  • the solid fraction thus treated is supplied to a compacting step following hydrolysis and/or aerobic drying.
  • the solid matter presenting a certain particle diameter is pressed into a predetermined geometrical shape, for example pellets or briquets.
  • This compacting step results in further dewatering of the mixture of substances to be treated, so that following compacting a dry-stable body is present which cannot be eluted any further.
  • This body may, for example, be stored as a substitute fuel being an alternative for fossile energy carriers, or in a garbage dump.
  • water is customarily used which is recycled in the process of the invention.
  • the air for hydrolysis and thermophilic drying of the mixture of substances may be guided in counterflow to the mixture of substances but also in parallel flow.
  • FIG. 1 is a sectional view of a reactor in which hydrolysis of a mixture of substances containing organic constituents takes place;
  • FIG. 2 shows a reactor for performing aerobic, thermophilic drying
  • FIG. 3 shows an installation having a plurality of hydrolysis and drying reactors in accordance with FIGS. 1 and 2 arranged in sequence;
  • FIG. 4 shows a device having a plurality of reactors for hydrolysis and/or drying arranged in sequence in a commnon container
  • FIG. 5 is a top view of the device of FIG. 4.
  • FIGS. 6 and 7 show alternative embodiments of a reactor.
  • FIG. 1 shows a process diagram explaining the process of the invention and the device for carrying out the process. Accordingly, the aerobic hydrolysis (aerobic biogenic reaction and percolation) takes place in a reactor 1 to which the mixture of substances 2 to be processed is supplied through a material feeding means 4 .
  • the mixture of substances to be processed contains a large proportion of structured material and organic matter. The like mixtures of substances occur, for example, in household waste, biological waste, industrial waste etc.
  • the reactor 1 is designed as a closed container, so that the material flows described in more detail hereinbelow are supplied via lock means, valve means etc.
  • the reactor 1 proper preferably is a steel or concrete container that is supplied from above with the mixture of substances (residual waste) in the shown embodiment.
  • a substantial proportion of the organic fraction of the mixture of substances consists of short-chained compounds that are mostly absorbed on a surface. If this surface is surrounded by a flow of warm water, primarily non-soluble compounds are also hydrolyzed and washed out.
  • the hydrolysis degree depends on the dwelling time in the reactor 1 .
  • the smell-intensive components of the mixture of substances and the hydrolysis products are well water-soluble and may be washed out. By percolation one therefore achieves a reduction of the organic matter and a deodorization of the mixture of substances. Together with the leaching fluid (process water), fine sand particles are furthermore carried oft.
  • the reactor 1 is closed so as to be smell tight, and the exhaust air is deodorized in the manner described more closely hereinbelow.
  • process air is additionally supplied, whereby the physico-chemical effect of water extraction is enhanced by intensifying the bacterial decomposition in the aerobic environment, the micro-organisms begin to excrete exoenzymes which split particle-shaped polymer components into monomers and solubilize them.
  • the charging means 4 is positioned at the upper end section of the reactor 1 when viewed in the direction of gravity.
  • At least one discharge means 6 is formed through which the processed and biologically decomposed mixture of substances may be withdrawn from the reactor 1 .
  • the reactor 1 moreover comprises below the discharge means 6 (representation of FIG. 1) a collector 10 which is separated from a reaction chamber 12 by a sieve floor 8 .
  • the discharge means 6 which shall be described in more detail hereinbelow, is designed such that the mixture of substances resting on the sieve floor 8 is discharged from the reactor in a layered configuration, and the openings of the sieve floor 8 are kept unobstructed.
  • the collector 10 communicates with an air connection duct 14 and a leaching fluid exit 16 .
  • another air connection duct 18 and a leaching agent distributor 20 are arranged.
  • the leaching fluid (water) used for percolation or extraction of the organic constituents of the mixture of substances is fed into the reactor through the distributor 20 and withdrawn through the exit 16 .
  • the floor 22 of the reactor 1 is inclined towards the exit 16 , so that the leaching fluid gathers in the range of the exit 16 .
  • the lower air connection duct 14 in the representation of FIG. 1 is connected with air conveying means 24 .
  • air conveying means fan, compressor
  • a flow 25 from the lower air connection duct 14 to the upper air connection duct La or a flow 27 in a reverse direction from the upper air connection duct 18 to the lower air connection duct 14 may be adjusted inside the reactor 1 .
  • the flow of leaching fluid takes place in the direction of gravity, namely, from the distributor 20 disposed in an upper location in the reactor 1 towards the exit 16 .
  • the leaching fluid exiting from the reactor 1 is treated by means of a sewage treatment device 26 (anaerobic filter) described in more detail in the following, and then recirculated to the distributor 20 .
  • a sewage treatment device 26 anaerobic filter
  • the residue resting on the sieve floor 8 is withdrawn as discharge material 28 through the discharge means 6 and either supplied to further processing as a product 30 or, in turn, recycled to the charging means 4 als circulation material 32 .
  • the separation of the discharge material 28 into product 30 and/or circulation material 32 takes place through a suitable apportioning means 34 which may, for example, have the form of a slide gate, trap, distributing guide etc.
  • a part of the discharge material 28 may be recirculated into the reactor 1 als circulation material 32 and may there be utilized for inoculation of the mixture of mubstances and thus for accelerating the biological decomposition.
  • the incoming mixture of substances 2 has in advance been treated mechanically in a known manner so as to have a predetermined maximum particle size.
  • This processed mixture of substances 2 is supplied via suitable conveying means, for example conveyor belts 36 , to the charging means 4 whereby a distribution of the mixture of substances 2 across the reactor cross-section takes place.
  • the charging means 4 includes a transversal conveyor 8 whereby the mixture of substances is distributed in the plane of drawing and in a transversal direction relative to the plane of drawing, and supplied to the reactor 1 by material hoppers 40 which are distributed over the cross-section.
  • the mixture of substances 2 is introduced into the reactor 1 in layers, so that practically n-layers 42 are arranged on the sieve floor 8 on top of each other.
  • the filling height H of the reactor 1 is selected such that the distributor 20 for the leaching fluid is located above the bulk material.
  • the distributor 20 may, for example, present a multiplicity of spraying heads 44 distributed across the reactor cross-section, whereby the leaching fluid may be distributed homogeneously over the topmost layer 42 .
  • the discharge means 6 has the form of a horizontal conveyor designed such that the respective bottom layer of the mixture of substances resting on the sieve floor 8 may be discharged in a horizontal direction.
  • the discharge means 6 has the form of a sliding or scraper floor as described, for example, in WO 95/20554 A1.
  • the like sliding floors are, for example, employed in sewage sludge silos, composting installations etc. and are known from the prior art, so that only the essential components shall be described hereinbelow.
  • the sliding floor includes a plurality of conveyor wedges 46 spaced apart in a horizontal direction (view of FIG. 1) and arranged on a thrust rod 48 .
  • the thrust rod 48 may be moved reciprocally, in parallel with arrows 52 , 54 in FIG. 1 with the aid of a hydraulic cylinder 50 or some other drive means.
  • the front surfaces of the conveyor wedges 46 facing the discharge opening have the form of vertical surfaces 56 , whereas the rear surfaces are inclined surfaces 58 .
  • the thrust rod 48 is periodically moved back and forth, wherein during the movement of the thrust rod 48 in the direction of arrow 52 (to the left in FIG. 1) the mixture of substances of the lowest layer slides upwards along the inclined surface 58 and comes to lie in the space behind the respective conveyor wedge 46 .
  • this material is carried along by the vertical surface 56 and conveyed to the right to the neighboring conveyor wedge 46 or to the discharge opening.
  • the height of the conveyor wedges 46 determines the height of the layers of the discharged mixture of substances.
  • the layer thickness of the discharge material about corresponds to the layer thickness of the material supply, with the filling height H accordingly remaining essentially constant.
  • a part of the discharge material 28 may be recycled to the conveyor means 36 or directly to the charging means 4 as inoculation material (circulation material 32 ).
  • inoculation material (circulation material 32 ).
  • all of the discharge material 28 als circulation material 32 , in which case the mixture of substances passes through the reactor 1 several times and is only discharged as product 30 following, for example, 4 runs.
  • the sieve floor 8 arranged underneath the discharge means 6 has a mesh size Z selected as a function of the composition and particle size of the mixture of substances to be processed.
  • the construction of the thrust rod 48 and of the conveyor wedges 46 is selected such that the sieve floor 8 is cleaned by the reciprocating movement of the scraper floor, so that an obstruction of the meshes may be prevented.
  • Layered discharge of material results in a movement of layers of the mixture of substances from top to bottom through the reactor 1 in a vertical direction (FIG. 1 ).
  • the air conveying means 24 may have the form of a fan or compressor, 80 that different directions of air flow may be adjusted in the reactor 1 .
  • the entry and exit ranges of the reactor 1 are selected such that the air flows through the layered mixture of substances while being distributed over the entire reactor cross-section. This air flow is indicated by dashed lines in the representation of FIG. 1 .
  • the leaching fluid flows through the layered mixture of substances along the solid-line arrows from top to bottom and enters, laden with organic matter, into the collector 10 through the sieve floor 8 .
  • the laden leaching fluid 60 is withdrawn via the exit 16 and supplied to the sewage treatment device 26 .
  • the latter comprises a foreign matter separator 62 in which foreign matter 64 such as, for example, sand, pebbles, suspended matter, float matter etc. are separated out.
  • Such foreign matter separators may, for example, comprise a settling tank and a skimmer for separating out the mentioned foreign matter 64 .
  • the leaching fluid freed from the foreign matter and containing colloidal organic compounds in aqueous phase is then supplied to an anaerobic automatter 66 , for example a biogas or digestion tower installation.
  • Metabolic end products produced in this anaerobic waste water treatment are methane and carbon dioxide and in some cases small amounts of hydrogen sulfide.
  • This biogas obtained as a decomposition product may be converted into electricity and heat in suitable block-type thermal power stations. A part of the energy recovered from the biogas is returned into the process of the invention which is thus largely self-sufficient as regards energy.
  • a sewage water purification plant is associated with the reactor.
  • the leaching fluid might also be incorporated into an existing sewage purification plant, or be introduced directly into the sewers, or supplied to another treatment step.
  • fresh water or industrial process water or weakly loaded sewage water will be used in that case.
  • the anaerobic fermenter 66 is followed immediately by a two-stage aerobic after treatment 70 , wherein digestion process water from the biogas installation is subjected to an after treatment for minimizing the residual load, and nitrogen is eliminated.
  • the loaded sewage 72 thereby produced is supplied to a further treatment stage or directly introduced into the sewer system.
  • the leaching fluid purified in the aerobic biological stage 70 is then supplied to the reactor 1 by way of the distributor 20 .
  • a partial flow of the digestion process water may be supplied directly from the anaerobic fermenter 66 to the distributor while bypassing the 2-stage aerobic biological stage 70 , in order to exert a catalytic influence on biological decomposition in the reactor 1 .
  • Decomposition of the organic materials is due, on the one hand, to the aerobic decomposition of the available carbon C into CO 2 (carbonic acid) and on the other hand to leaching out of the dissolved and acidified organic matter and removal by way of the leaching fluid. Due to the aerobic, thermophilic reaction and the simultaneous decomposition of the organic compounds, the temperature in the mixture of substances rises (to approx. 40 to 50° C., for example) during the extracting step. As a result of this temperature increase water vapor is liberated, which is discharged via the supplied air. This water vapor discharged together with the air may be supplied to the above described sewage water purification as a condensate.
  • the air flowing off from the reactor 1 is laden with carbon dioxide as a decomposition product and with the water vapor produced by the heating.
  • the exhaust air laden with organic components may be supplied to a biofilter wherein biological cleaning by means of aerobic micro-organisms takes place.
  • the mixture of substances 2 located inside the reactor 1 is subjected to intermittent pulses due to the reciprocating movement of the conveyor wedges 46 , whereby shear, transversal and longitudinal forces are introduced into the mixture of substances and possibly formed flow channels of the leaching fluid and of the air are destroyed.
  • the magnitude of these forces is designed such as to be capable of destroying these channels and chimneys on the one hand, however not to result in destruction of the layered structure.
  • these pulses are brought about by the movement of the scraper floor; as an alternative, however, as is represented in FIGS. 6 and 7, additional means for inducing shear forces in the mixture of substances 2 and for destroying the Channels might be employed, as represented in FIGS. 6 and 7.
  • the discharge material 28 is supplied to a drying step. It was found to be particularly advantageous if this drying takes place as aerobic drying, for the residual humidity may then be reduced at minimum energy expense.
  • aerobic drying may be effected, for example, by interrupting the supply of leaching fluid through the distributor 20 , so that nothing but air flows through the mixture of substances 2 following hydrolysis. As a result of flow through the humid mixture of substances 2 , further aerobic decomposition of the as yet available carbon C into carbon dioxide takes place.
  • the mixture of substances is heated due to the microbial conversion and thereby water vapor is discharged by way of the flow of air passing through. Due to the aerobic decomposition of the carbon and discharge of the water vapor, the residual humidity of the mixture of substances is reduced, with the desired proportion of dry substrate being adjustable in a simple manner through the duration of aerobic drying.
  • hydrolysis and aerobic drying are thus performed in a single reactor 1 .
  • the reactor 1 may be used both for drying and percolation without any modification, so that a simple structure of the installation is ensued.
  • This aerobic dryer 74 essentially has the same construction as the reactor 1 of FIG. 1, i.e. the mixture of substances, in this case the discharge material 28 , is introduced via a charging means 4 into a container provided with lock means, and following completed aerobic drying is discharged via a discharge means 6 .
  • the dryer 74 has a plurality of air connection ducts 14 arranged above each other perpendicularly to the plane of drawing, so that the air may be injected in sheet form. The drying air, in turn, may be guided in counterflow or in parallel flow with the flow of the mixture of substances and is accordingly supplied and discharged through air connection ducts 14 , 16 .
  • the dryer 74 of FIG. 2 does not include a distributor 20 for the application of leaching fluid.
  • the aerobic dryer 74 in turn, partial recirculation of the dry material 76 present at the exit from the dryer 74 as circulation material 78 and/or discharge of a dried product 80 is provided for.
  • the mixture of substances to be dried passes through the dryer 74 , once again preferably in a layered form, with channel formation being suppressed by shear, transversal and longitudinal forces applied in the form of pulses.
  • This 2-stage process might, of course, be carried out by means of two reactors arranged in sequence in accordance with FIG. 1, with hydrolysis in the first reactor taking place through supplying air and leaching fluid, whereas in the second, downstream reactor 1 only aerobic drying an a result of supplying air takes place.
  • FIG. 3 shows an embodiment wherein three reactors 1 a , 1 b , 1 c in accordance with FIG. 1 are combined with three dryers 74 a , 74 b , 74 c in accordance with FIG. 2 .
  • a common conveyor means 36 is associated to the three reactors 1 a , 1 b , 1 c , whereby the mixture of substances 2 may be supplied to the single reactors 1 a , 1 b , 1 c .
  • suitable apportioning means 34 in turn, the flow of material to the single reactors 1 a , 1 b , 1 c may be adjusted.
  • the discharge material 28 a , 28 b , 28 c from the single reactors 1 a , 1 b , 1 c may in turn be recirculated by way of the apportioning means 34 als circulation material 34 or, in turn, supplied as product 30 to further processing, or as discharge material 28 to the aerobic drying.
  • the discharge material 28 from reactors 1 a , 1 b , 1 c is supplied to the dryers 74 a , 74 b , 74 c through conveyor means 84 and suitable apportioning means 34 .
  • the mixture of substances 2 is also supplied to drying directly, i.e. while bypassing the reactors 1 .
  • This is the case, for example, when the mixture of substances present already includes a considerable proportion of dry substance, so that no more wet washing takes place.
  • the discharge material from the dryers 74 i.e. the dry material 76 a , 76 b , 76 c is then either further processed as dry product 86 , again supplied to drying as circulation material 78 , or supplied to means 90 for dewatering and/or compacting as an intermediate product 88 .
  • the means 90 is also used for further processing of the discharge material from the reactors/dryers represented in FIGS. 1, 2 .
  • the means 90 may, for example, have the form of an extruder or a dryer/extruder press so that as a result of the mechanical action and the heat generated by the pressure buildup, further dewatering or drying of the intermediate product 88 takes place.
  • the extracted residual waste is adjusted to a dry substance content of >60%.
  • the means 90 moreover contains a high-performance press whereby the extracted, dewatered material may be pelleted.
  • densities of 1.7 t/m 3 are attained.
  • the energy expense for producing the pellets amounts to approx. 1% of the energy content of the pellets when one assumes a mean energy content of 14 MD/kg.
  • the dewatered final product 92 may be present as a pellet, briquet or in another compacted form.
  • a product may be produced which cannot be eluted further, has no breathing activity, and is characterized by a large proportion of dry substance, wherein it is not necessary to employ thermal energy from the outside for drying in contrast with the known process.
  • the material dewatered with the aid of the means 90 may be subjected to subsequent drying by means of composting or belt drying.
  • Conventionally post-rotting was previously connected after a mechanical-biological treatment of waste in order to attain additional decomposition of organic material and drying of the leached residue. Post-rotting may readily take place in an exposed pit.
  • the proportion of biogenic material is sufficiently high even after percolation, so that the rotting temperature will rise to 70° C. within 4 to 6 days. Within 10 to 16 days the residue thus treated attains a dry substance content of up to 80%.
  • waste heat for drying of the percolation residue would be available in the above described process owing to biogas extraction and conversion into electricity in a gas engine, a space-saving drying process may also be employed for post-rotting.
  • the arrangement represented in FIG. 3 is selected when a continuous operation is desired. At high throughputs, the installation may be expanded by adding further modules (reactors 1 , dryers 74 ).
  • the conveying means 36 and 84 and the apportioning means 34 may be controlled such that the order of charging, emptying or mixing (circulation material) of the single reactors, dryers may be changed in any desired order.
  • a common conveyor means 36 is associated whereby the mixture of substances 2 to be processed is supplied to the container 96 .
  • the common conveyor means 36 the mixture of substances is guided via the apportioning means 34 to a transversal conveyor 38 having the form of a distributor crane in the shown embodiment.
  • the latter includes a material chute 40 which is movable across the entire cross-sectional area of the container 96 by means of the distributor crane (transversal conveyor 38 ).
  • the distributor crane transversal conveyor 38
  • Discharging the treated mixture of substances takes place. through a discharge means 6 which may, for example, be designed like the one in FIG. 1 .
  • a discharge means 6 which may, for example, be designed like the one in FIG. 1 .
  • the container 96 has the form of a multiple-chamber dryer designed to have air connection ducts 14 , 18 , with only the air connection duct 18 arranged on top being shown in FIG. 4 .
  • the container 96 might, of course, also be designed as a reactor having a plurality of partial chambers.
  • the reactors/dryers represented in FIGS. 1 to 3 may, of course, also be designed to include a plurality of laterally adjacent discharge means 6 .
  • the discharge material 28 may be returned to the conveyor means 36 via the apportioning means 34 as circulation material 32 , or, however, be discharged as product 30 .
  • FIG. 5 shows a top view of the container 36 of FIG. 4 explaining distribution of the mixture of substances 2 .
  • the mixture of substances 2 is charged on the conveyor means 36 , for example a conveyor belt, and thereby supplied to a distributor crane 38 that is movable in the direction of arrows 100 , 101 above the partition walls 98 , 99 .
  • the distributor crane 38 carries one movable or a plurality of stationary material chutes 40 , so that the entire width (vertical FIG. 5) of the partial chambers 1 a , 1 b , 1 c may be covered.
  • the processed mixture of substances is discharged from the container 96 in the direction of arrow 102 , and this discharge material 28 is carried off through suitable conveyor means either as product 30 or as circulation material 32 .
  • suitable conveyor means either as product 30 or as circulation material 32 .
  • the latter is transported back to the conveyor means 36 by a conveyor belt and then once more charged into one of partial spaces 1 a , 1 b , 1 c.
  • the process air was injected into the bottom portion of the reactor 1 or dryer, respectively, through one or a plurality of air connection ducts 14 and then enters through the sieve floor 8 into the heap material (bulk material).
  • the process air is injected through a multiplicity of lances 110 distributed over the crosssection of the reactor 1 , the nozzles 112 of which open into the lower range (view of FIGS. 6, 7 ) of the bulk material 114 .
  • the lances 110 extend through the sieve floor 8 and the discharge means 6 —in the present case the sliding floor.
  • the lances 110 for process air or pressurized air are each connected through a control valve 116 to a pressure line 118 which opens into a pressure accumulator 120 .
  • the latter is connected to a compressor 122 through which fresh air or air 124 recycled from the exhaust air treatment (biofilter) may be taken to the system pressure, i.e. the pressure in the pressure accumulator 120 .
  • the control valves 116 are connected to a process control means 126 and may thus individually be controlled open and closed, respectively.
  • the opening cross-section of the control valves 116 may be continuously variable depending on the process control means 126 , so that the pressure of the process/pressure gas is variable.
  • the system pressure in the pressure accumulator 120 is preferably adjusted to a pressure of more than 4 bar.
  • pressurized air 128 exits from the nozzle opening in an upwardly direction (view of FIGS. 6, 7 ) and flows through the bulk material 114 in a vertical direction at the maximum pressure, with the arrows in FIGS. 6, 7 indicating that the pressurized air 128 is also deflected in the transversal direction.
  • the bulk material 114 is partially whirled up or fluidized in the range through which the pressurized air 128 flows, so that the surfaces of the heap material are reformed and channels are destroyed.
  • a partial undulating movement 130 is generated in the bulk material 114 , which moves away from the nozzle 112 of the respective lance 110 through the bulk material 114 in an upwardly direction. Due to this undulating movement, a relative movement of the mixture of substances is induced, so that the surfaces of the particles are torn open and thus the mass transfer area is increased.
  • the pressurized air is only injected in pulses, the bulk material 114 again collapses after the control valves 116 are closed, no that again shear forces are introduced into the bulk material 114 which result in repeated reformation of the surfaces and in destruction of channels.
  • the laden air 123 exiting from the reactor 1 is supplied to a biofilter.
  • the process control 126 and the control valves 116 are designed such that the pressure of the process/pressurized air may be varied over time, so that for example over a predetermined time interval process air only having a low pressure (0.5 bar) is supplied which is required for drying or hydrolysis, however does not result in considerable introduction of shear forces into the bulk material 114 .
  • pressurized air is then intermittingly supplied at a comparatively high pressure (>4 bar) in order to introduce the above described shear forces and avoid a formation of channels.
  • valves 116 of the multiplicity of pressure lances 110 of the reactor 1 may also be controlled consecutively, so that an “expansion wave” propagating in parallel with the plane of drawing or perpendicularly to the plane of drawing in the representation according to FIGS. 6 and 7 passes through the bulk material.
  • the embodiment represented in FIG. 6 corresponds to the above described embodiments.
  • the mixture of substances 2 is introduced into the reactor 1 by way of the charging means 4 from above in a layered configuration and migrates through the latter, with the layered structure remaining substantially unchanged due to the supply of pressurized air and the resulting partial fluidization of the bulk material.
  • the processed mixture of substances is then discharged via the discharge means 6 , i.e. a sliding floor, and supplied to the further treatment steps.
  • the mixture of substances 2 is supplied at the left-hand front face of the reactor 1 in the representation of FIG. 7 and is at the opposite side of the reactor 1 discharged in a downwardly direction. Accordingly, the mixture of substances migrates through the reaction chamber 12 having a vertically arranged layered structure as is designated by reference symbols l l to l n . I.e., the mixture of substances moves through the reactor in a horizontal direction (l) while being displaced through the reactor in a vertical direction in the embodiment represented in FIG. 6 .
  • FIGS. 6 and 7 correspond to the above described embodiments, so that reference is made to the above explanations with regard to the remaining components.
  • the same reference numerals were used in FIGS. 6 and 7 for corresponding components as in FIGS. 1 to 5 .
  • the agitator used in the prior art was replaced with a “pressurized air agitator”, with the pressure for the pressurized air being selected such that the layered structure is essentially preserved.
  • the bulk material 114 may purposely be subjected to pressure pulses, so that the introduction of shear forces may be applied depending on the process, i.e., application of pressurized air v. process air may be effected as a function of the quality of the mixture of substances to be processed and of the dwell time in the reactor 1 .
  • the applicant reserves the right of directing independent sets of claims to the variants represented in FIGS. 6 and 7 and 1 to 5 .
  • a process for treating a mixture of substances containing structured constituents and organic matter, and a device for carrying out this process are disclosed.
  • the mixture of substances is subjected to pulse-type or periodical application of force, so that the formation of flow channels for a leaching fluid or process air in a bulk material may be prevented.

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DE19851306 1998-11-06
DE19851306 1998-11-06
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DE19909353 1999-03-03
PCT/IB1999/001950 WO2000027777A1 (de) 1998-11-06 1999-11-04 Verfahren und vorrichtung zur aufbereitung eines organik enthaltenden stoffgemisches

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US20040177451A1 (en) * 2001-08-08 2004-09-16 Philippe Poulin Composite fibre reforming method and uses
US20040192980A1 (en) * 2003-03-28 2004-09-30 Appel Brian S. Process for conversion of organic, waste, or low-value materials into useful products
US20050035058A1 (en) * 2003-08-14 2005-02-17 Forrestal Brian Joseph System for the production of biogas and compost from organic materials and method of operating an organic treatment facility
US20050113611A1 (en) * 2003-03-28 2005-05-26 Adams Terry N. Apparatus and process for separation of organic materials from attached insoluble solids, and conversion into useful products
US20070098625A1 (en) * 2005-09-28 2007-05-03 Ab-Cwt, Llc Depolymerization process of conversion of organic and non-organic waste materials into useful products
US20090062581A1 (en) * 2003-03-28 2009-03-05 Appel Brian S Methods and apparatus for converting waste materials into fuels and other useful products
US20090155892A1 (en) * 2005-09-08 2009-06-18 Peter Lutz Bioreactor comprising a retaining system
US20090173123A1 (en) * 2006-05-17 2009-07-09 Charles William Douglas Blandy Integrated power generation and organic fertiliser production system
US20100055767A1 (en) * 2004-12-02 2010-03-04 O'kane Pearse Bio-energy system and apparatus
US20100311155A1 (en) * 2007-12-06 2010-12-09 Jorgen Ejlertsson Method for treatment of organic material
EP2275394A1 (en) * 2008-04-08 2011-01-19 Taniguro, Katsumori Method and apparatus for treating organic waste and method of utilizing heat energy
US20110239716A1 (en) * 2008-10-17 2011-10-06 Koji Miyanouchi Useful product producing apparatus, useful product produced by same and method for producing useful product
US8329455B2 (en) * 2011-07-08 2012-12-11 Aikan North America, Inc. Systems and methods for digestion of solid waste
CN103230930A (zh) * 2013-05-14 2013-08-07 戴道国 垃圾发酵出料装置
US8759083B2 (en) 2006-02-21 2014-06-24 Bekon Energy Technologies Gmbh & Co., Kg Bioreactor for methanization of biomass having a high solids fraction
US8969426B2 (en) 2010-05-02 2015-03-03 Dynasep Inc. Method for the preparation of highly purified recycled nylon
US9096822B2 (en) * 2012-01-18 2015-08-04 Zero Waste Energy, LLC. Device to produce biogas
US9139790B2 (en) 2009-10-07 2015-09-22 Katsumori Taniguro Method for treating biomass material and method for using heat energy
US10577289B2 (en) * 2018-01-13 2020-03-03 Earnest Earth Agriculture, Inc. Vermiculture bioreactor system and method of use
US11065656B2 (en) * 2016-06-27 2021-07-20 Shinko Tecnos Co., Ltd. Method and apparatus for producing a product
US20210323038A1 (en) * 2019-12-31 2021-10-21 Xi'an Shiyou University Remediation simulator of deep petroleum contaminated soil and application
RU2817456C2 (ru) * 2022-09-20 2024-04-16 Федеральное государственное бюджетное научное учреждение "Федеральный научный агроинженерный центр ВИМ" (ФГБНУ ФНАЦ ВИМ) Секционная сушилка периодического действия открытого типа

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FI13268Y1 (fi) * 2022-06-04 2022-09-22 Oy Raita Env Ltd Syväkompostointilaite
CN115805029B (zh) * 2023-01-11 2023-05-23 山西黄腾化工有限公司 一种抗絮凝剂的制备装置及其制备方法

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US7651852B2 (en) * 2000-10-26 2010-01-26 Anaeco Limited Method and apparatus for aerating organic waste material
US20040016274A1 (en) * 2000-10-26 2004-01-29 Thomasz Rudas Method and apparatus for aerating organic waste material
US7960172B2 (en) 2000-10-26 2011-06-14 Anaeco Limited Method and apparatus for aerating organic waste material
US20090013741A1 (en) * 2000-10-26 2009-01-15 Anaeco Limited Method and apparatus for aerating organic waste material
US20040177451A1 (en) * 2001-08-08 2004-09-16 Philippe Poulin Composite fibre reforming method and uses
US7288317B2 (en) * 2001-08-08 2007-10-30 Centre National De La Recherche Scientifique Composite fibre reforming method and uses
US8877992B2 (en) 2003-03-28 2014-11-04 Ab-Cwt Llc Methods and apparatus for converting waste materials into fuels and other useful products
US20050113611A1 (en) * 2003-03-28 2005-05-26 Adams Terry N. Apparatus and process for separation of organic materials from attached insoluble solids, and conversion into useful products
US20090062581A1 (en) * 2003-03-28 2009-03-05 Appel Brian S Methods and apparatus for converting waste materials into fuels and other useful products
US8809606B2 (en) 2003-03-28 2014-08-19 Ab-Cwt Llc Process for conversion of organic, waste, or low-value materials into useful products
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US8003833B2 (en) 2003-03-28 2011-08-23 Ab-Cwt, Llc Process for conversion of organic, waste, or low-value materials into useful products
US20050035058A1 (en) * 2003-08-14 2005-02-17 Forrestal Brian Joseph System for the production of biogas and compost from organic materials and method of operating an organic treatment facility
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US20100055767A1 (en) * 2004-12-02 2010-03-04 O'kane Pearse Bio-energy system and apparatus
US20090155892A1 (en) * 2005-09-08 2009-06-18 Peter Lutz Bioreactor comprising a retaining system
US8053228B2 (en) * 2005-09-08 2011-11-08 Bekon Energy Technologies Gmbh & Co., Kg Bioreactor comprising a retaining system
US20070098625A1 (en) * 2005-09-28 2007-05-03 Ab-Cwt, Llc Depolymerization process of conversion of organic and non-organic waste materials into useful products
US7771699B2 (en) 2005-09-28 2010-08-10 Ab-Cwt, Llc Depolymerization process of conversion of organic and non-organic waste materials into useful products
US8759083B2 (en) 2006-02-21 2014-06-24 Bekon Energy Technologies Gmbh & Co., Kg Bioreactor for methanization of biomass having a high solids fraction
US20090173123A1 (en) * 2006-05-17 2009-07-09 Charles William Douglas Blandy Integrated power generation and organic fertiliser production system
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US20100311155A1 (en) * 2007-12-06 2010-12-09 Jorgen Ejlertsson Method for treatment of organic material
US20110021862A1 (en) * 2008-04-08 2011-01-27 Katsumori Taniguro Method for treating organic waste and method of utilizing heat energy
EP2275394A4 (en) * 2008-04-08 2013-01-02 Taniguro Katsumori METHOD AND DEVICE FOR TREATING ORGANIC WASTE AND METHOD FOR UTILIZING HEAT ENERGY
US9321698B2 (en) * 2008-04-08 2016-04-26 Katsumori Taniguro Method for treating organic waste and method of utilizing heat energy
EP2275394A1 (en) * 2008-04-08 2011-01-19 Taniguro, Katsumori Method and apparatus for treating organic waste and method of utilizing heat energy
US20110239716A1 (en) * 2008-10-17 2011-10-06 Koji Miyanouchi Useful product producing apparatus, useful product produced by same and method for producing useful product
US9139790B2 (en) 2009-10-07 2015-09-22 Katsumori Taniguro Method for treating biomass material and method for using heat energy
US8969426B2 (en) 2010-05-02 2015-03-03 Dynasep Inc. Method for the preparation of highly purified recycled nylon
US9328323B2 (en) 2011-07-08 2016-05-03 Aikan North America, Inc. Systems and methods for digestion of solid waste
CN104024181A (zh) * 2011-07-08 2014-09-03 艾肯北美公司 用于消化固体废弃物的系统及方法
US8492134B2 (en) 2011-07-08 2013-07-23 Aikan North America, Inc. Systems and methods for digestion of solid waste
US8329455B2 (en) * 2011-07-08 2012-12-11 Aikan North America, Inc. Systems and methods for digestion of solid waste
US9096822B2 (en) * 2012-01-18 2015-08-04 Zero Waste Energy, LLC. Device to produce biogas
CN103230930B (zh) * 2013-05-14 2015-09-09 戴道国 垃圾发酵出料装置
CN103230930A (zh) * 2013-05-14 2013-08-07 戴道国 垃圾发酵出料装置
US11065656B2 (en) * 2016-06-27 2021-07-20 Shinko Tecnos Co., Ltd. Method and apparatus for producing a product
US10577289B2 (en) * 2018-01-13 2020-03-03 Earnest Earth Agriculture, Inc. Vermiculture bioreactor system and method of use
US20210323038A1 (en) * 2019-12-31 2021-10-21 Xi'an Shiyou University Remediation simulator of deep petroleum contaminated soil and application
RU2817456C2 (ru) * 2022-09-20 2024-04-16 Федеральное государственное бюджетное научное учреждение "Федеральный научный агроинженерный центр ВИМ" (ФГБНУ ФНАЦ ВИМ) Секционная сушилка периодического действия открытого типа

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DE19982310D2 (de) 2001-11-29
AU768296B2 (en) 2003-12-04
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JP4212241B2 (ja) 2009-01-21
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NZ512168A (en) 2003-11-28
AU1402500A (en) 2000-05-29
EP1127034A1 (de) 2001-08-29
PT1127034E (pt) 2003-09-30
PL348639A1 (en) 2002-06-03
JP2002529232A (ja) 2002-09-10
HRP20010317A2 (en) 2002-06-30
CN1325370A (zh) 2001-12-05
ATE240282T1 (de) 2003-05-15
SK6122001A3 (en) 2001-12-03
EP1127034B1 (de) 2003-05-14
ID29851A (id) 2001-10-18
CZ20011509A3 (cs) 2002-04-17
HK1037603A1 (en) 2002-02-15
CA2349946A1 (en) 2000-05-18
SK285015B6 (sk) 2006-04-06
DK1127034T3 (da) 2003-08-25
CA2349946C (en) 2007-10-30
WO2000027777A1 (de) 2000-05-18

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